CN106904710B - Application device of flocculating agent spiral pipeline - Google Patents
Application device of flocculating agent spiral pipeline Download PDFInfo
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- CN106904710B CN106904710B CN201710193006.9A CN201710193006A CN106904710B CN 106904710 B CN106904710 B CN 106904710B CN 201710193006 A CN201710193006 A CN 201710193006A CN 106904710 B CN106904710 B CN 106904710B
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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Abstract
A spiral pipeline of flocculating agent, preparation method and its application, the spiral pipeline is made up by many macromolecule materials; the method comprises the following steps: carrying out esterification reaction on various macromolecular materials for 22-32 hours; sequentially irradiating by alpha rays and beta rays; keeping the temperature in the reaction kettle and standing for 32-42 hours; the stirrer is set to rotate at a set speed for stirring, and the pressure of the reaction kettle is reduced to 0 MPa; adding a cross-linking agent, stirring and mixing, and standing for 12-32 hours at a constant temperature; the pressure of the reaction kettle is increased to 2.12MPa to 2.92MPa, the temperature is 152 ℃ to 272 ℃, and the polymerization reaction is carried out for 22 hours to 32 hours; reducing the pressure in the reaction kettle to 0MPa, reducing the temperature to 32-52 ℃, discharging, and putting into a molding press to prepare the spiral pipeline of the flocculating agent. The application comprises the following steps: as a component of a sewage treatment device. The spiral flocculating agent pipeline, the preparation method and the application can obtain the spiral flocculating agent pipeline with excellent quality, and the application can improve the sewage treatment efficiency.
Description
Technical Field
The invention relates to the field of sewage treatment application, in particular to a spiral pipeline of a flocculating agent, a preparation method and application thereof.
Background
The sewage coagulation filler is a device for adding substances such as flocculating agent and the like into sewage to realize fluid flocculation and rapid sedimentation, and the sewage is converted into sediment from high-speed fluid so as to reach the specified discharge index. Meanwhile, the device is also one of the main devices for improving the removal rate of the sewage pollutants.
The data show that the market scale of the domestic sewage coagulation filler industry in 2015 is about 500 million yuan, and the domestic sewage coagulation filler industry is mainly concentrated in the fields of domestic sewage, chemical industry, metallurgy, medicine, ships, machinery, food processing and the like. Based on the increase of the stable demand of industries such as petroleum, chemical industry, electric power, metallurgy, ships, machinery, food, pharmacy and the like on the sewage coagulation filler, the sewage coagulation filler industry in China will keep stable growth in a future period, during 2011-2020 years, the sewage coagulation filler industry in China will keep the growth of about 10-15% of the year, and the scale of the sewage coagulation filler industry in China is expected to reach 1500 billion yuan by 2020.
The domestic sewage coagulation filler industry obtains remarkable results in the aspects of saving energy, improving the efficiency, improving the treatment efficiency, reducing the treatment area, reducing the pressure drop, improving the strength of the device and the like. However, the existing sewage coagulation filler has low treatment efficiency, mainly because the added flocculating agent and coagulant aid cannot be fully mixed with sewage, the existing sewage coagulation filler is not particularly suitable for the requirement of large-scale water treatment; in addition, dirt generated in the sewage treatment process of the conventional sewage coagulation filler is not easy to clean, so that time and labor are wasted in the cleaning process of the sewage coagulation filler, and the sewage treatment efficiency is seriously reduced.
The spiral pipeline of the flocculating agent is an important component in the sewage coagulation filler, the performance of the spiral pipeline has very important influence on the sewage treatment efficiency, wherein the heat conductivity, high temperature resistance, high pressure resistance and corrosion resistance of the spiral pipeline of the flocculating agent are decisive factors, the heat conductivity of the existing spiral pipeline of the flocculating agent is poor, and the high temperature resistance, the high pressure resistance and the corrosion resistance are all low.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a spiral pipeline of a flocculating agent, a preparation method and application thereof, wherein the spiral pipeline of the flocculating agent has good heat conductivity, high temperature resistance, high pressure resistance and high corrosion resistance; the preparation method has simple process, is not easy to pollute the environment, and has lower requirements on technology and equipment; the application can obtain the sewage treatment equipment with high treatment efficiency, long service life and high reliability.
The invention provides a spiral pipeline of a flocculating agent, which comprises the following components in parts by weight:
72-132 parts of bis [2- [ [6- [ (4-chloro-6-methoxy-1, 3, 5-triazin-2-yl) amino ] -1-hydroxy-3-sulfo-2-naphthyl ] azo ] benzoic acid ] chromic acid disodium salt, 62-162 parts of [ 4-hydroxy-3- [ (2-hydroxy-5-nitro-3-sulfophenyl) azo ] -6- [ (sulfomethyl) amino ] -2-naphthalenesulfonato ] sodium chromate, 112-222 parts of 6- [ (5-chloro-2-hydroxy-3-nitrophenyl) azo ] -5-hydroxy-4-phenylamino-1-naphthalenesulfonate monosodium salt, and 112-222 parts of bis [ 6-amino-5- [ (2-hydroxy-3, 22-62 parts of 5-dinitrophenyl) azo ] -1-naphthalenesulfonate (3-1) ] cobalt (III) trisodium, 82-142 parts of N- (2-carboxyl-5-chlorphenyl) -6-methoxy-3-pyridylamine, 42-82 parts of 3-ethyl-5-methyl-4- (2-chlorphenyl) -2- (2, 2-diethoxy-ethoxymethyl) -6-methyl-1, 4-dihydro-pyridine-3, 5-dicarboxylic acid, 62-122 parts of 4-phenyl-6-methyl-5-ethoxycarbonyl-dihydropyridinone with the concentration of 32-62 ppm, and 5-methoxycarbonyl-4- (4-methoxyphenyl) -6-methyl-3, 42-82 parts of 4-dihydropyrimidine-2 (1H) ketone, 122-152 parts of 2, 3-dihydro-2-hydroxy-1, 3, 3-trimethyl-1H-indole-2-carbonyloxyaldehyde (4-methoxyphenyl) methylhydrazone, 72-172 parts of a crosslinking agent, 52-122 parts of 1,3, 3-trimethyl-2-methylene 2, 3-indoline, 32-92 parts of 5-chloro-1, 3, 3-trimethyl-2-methylindoline, 52-142 parts of 5- (4, 6-dimethoxypyrimidin-2-ylcarbamoylsulfamoyl) -1-methylpyrazole-4-carboxylic acid, 1- (4, 6-dimethoxypyrimidin-2-yl) -3- (3-dimethylcarbamoylpyridin-2-yl) Sulfonyl) urea 92-172 parts.
The spiral pipeline of the flocculating agent has good heat conductivity, high temperature resistance, high pressure resistance, high corrosion resistance, long service life and difficult damage.
Further, in order to improve various performances of the spiral pipeline of the flocculating agent, the crosslinking agent is any one of 6-ethoxy-3-pyridylmethylamine, 2-ethyl-6-methyl-3-hydroxypyridine and 2-hydroxyethyl-3-ethylpyridine.
A preparation method of a spiral pipeline of a flocculating agent comprises the following steps:
the method comprises the following steps: adding 1472-1742 parts of ultrapure water with the conductivity of 3.22 muS/cm-5.22 muS/cm into the reaction kettle, starting a stirrer in the reaction kettle at the rotating speed of 72 rpm-132 rpm, and starting a heating pump to raise the temperature in the reaction kettle to 52-82 ℃; sequentially adding bis [2- [ [6- [ (4-chloro-6-methoxy-1, 3, 5-triazine-2-yl) amino ] -1-hydroxy-3-sulfo-2-naphthyl ] azo ] benzoic acid ] chromic acid disodium salt, [ 4-hydroxy-3- [ (2-hydroxy-5-nitro-3-sulfophenyl) azo ] -6- [ (sulfomethyl) amino ] -2-naphthalenesulfonato ] sodium chromate and 6- [ (5-chloro-2-hydroxy-3-nitrophenyl) azo ] -5-hydroxy-4-phenylamino-1-naphthalenesulfonic acid monosodium salt, stirring until complete dissolution, adjusting the pH value to 4.2-7.2, adjusting the rotation speed of the stirrer to 142-262 rpm at the temperature of 112-152 ℃, and carrying out esterification reaction for 22-32 hours;
step two: crushing di [ 6-amino-5- [ (2-hydroxy-3, 5-dinitrophenyl) azo ] -1-naphthalenesulfonate (3-1) ] trisodium cobalt (III) and N- (2-carboxyl-5-chlorphenyl) -6-methoxy-3-pyridylamine into powder with the particle size of 532-1452 meshes; adding 3-ethyl-5-methyl-4- (2-chlorphenyl) -2- (2, 2-diethoxy-ethoxymethyl) -6-methyl-1, 4-dihydro-pyridine-3, 5-dicarboxylic acid, uniformly mixing, flatly paving in a tray, wherein the flatly paving thickness is 42-62 mm, and irradiating for 72-152 minutes by adopting alpha rays with the dose of 5.2-11.2 kGy and the energy of 6.2 MeV-15.2 MeV and beta rays with the same dose of 62-142 minutes;
step three: dissolving the mixed powder treated in the second step into 4-phenyl-6-methyl-5-ethoxycarbonyl-dihydropyridone, adding the mixture into a reaction kettle, wherein the rotating speed of a stirrer is 82-192 rpm, the temperature is 92-172 ℃, starting a vacuum pump to enable the vacuum degree of the reaction kettle to reach-0.04 MPa to-0.09 MPa, and keeping the state to react for 12-22 hours; releasing pressure and introducing radon gas to ensure that the pressure in the reaction kettle is between 1.32 and 1.72MPa, and keeping the temperature and standing for 32 to 42 hours; the rotating speed of the stirrer is increased to 162 rpm-312 rpm, and the pressure of the reaction kettle is reduced to 0 MPa; sequentially adding 5-methoxycarbonyl-4- (4-methoxyphenyl) -6-methyl-3, 4-dihydropyrimidine-2 (1H) ketone, 2, 3-dihydro-2-hydroxy-1, 3, 3-trimethyl-1H-indole-2-carboxaldehyde (4-methoxyphenyl) methylhydrazone to completely dissolve, adding a cross-linking agent, stirring and mixing to ensure that the hydrophilic-lipophilic balance value of the solution in the reaction kettle is 6.2-9.2, and standing for 12-32 hours under heat preservation;
step four: when the rotating speed of a stirrer is 152-232 rpm, sequentially adding 1,3, 3-trimethyl-2-methylene 2, 3-indoline, 5-chloro-1, 3, 3-trimethyl-2-methylindoline, 5- (4, 6-dimethoxypyrimidine-2-yl carbamoylsulfamoyl) -1-methylpyrazole-4-carboxylic acid and 1- (4, 6-dimethoxypyrimidine-2-yl) -3- (3-dimethylcarbamoylpyridine-2-yl sulfonyl) urea, and increasing the pressure of a reaction kettle to 2.12-2.92 MPa, the temperature of the reaction kettle is 152-272 ℃, and carrying out polymerization reaction for 22-32 hours; and after the reaction is finished, reducing the pressure in the reaction kettle to 0MPa, reducing the temperature to 32-52 ℃, discharging, and putting into a molding press to obtain the spiral pipeline of the flocculant.
The preparation method has simple process, easy realization, difficult environmental pollution and lower requirements on technology and equipment.
An application of spiral pipeline of flocculant as a component of sewage treating apparatus,
the sewage treatment device comprises a flocculation tank which is transversely arranged, wherein the upper part of the tank body of the flocculation tank is respectively provided with a coagulant aid liquid inlet pipeline and a flocculant liquid inlet pipeline, the lower part of the tank body of the flocculation tank is respectively provided with a cleaning agent liquid outlet pipeline and a flocculant liquid outlet pipeline, the left side and the right side of the tank body of the flocculation tank are respectively provided with a cleaning agent liquid inlet pipeline and a coagulant aid liquid outlet pipeline, a cleaning agent spraying mechanism, a filter disc and a coagulant aid straight pipeline are arranged inside the flocculation tank, and the flocculation tank is cylindrical; the filter disc is internally provided with at least one filter screen and divides the flocculation tank into a first chamber on the left side and a second chamber on the right side; the first chamber is provided with a sewage inlet pipeline communicated with the outside of the flocculation tank; a sewage discharge pipeline communicated to the outside of the flocculation tank is arranged at the right end of the second chamber; the cleaning agent spraying mechanism is positioned in the first chamber, a plurality of spray heads are uniformly arranged on the right side of the cleaning agent spraying mechanism, and inlet ends of the spray heads are communicated with a water outlet end of a cleaning agent liquid inlet pipeline penetrating into the flocculation tank; the cleaning agent spraying mechanism is arranged at the water outlet end of the cleaning agent inlet pipeline through a bearing; the coagulant aid straight pipeline is positioned in the second chamber; the number of the coagulant aid straight pipelines is multiple, the multiple coagulant aid straight pipelines extend along the length direction of the flocculation tank, liquid inlet ends of the multiple coagulant aid straight pipelines are communicated with one end of a coagulant aid liquid inlet pipeline penetrating into the flocculation tank, and liquid outlet ends of the multiple coagulant aid straight pipelines are communicated with one end of a coagulant aid liquid outlet pipeline extending into the flocculation tank; a plurality of liquid outlet holes I are uniformly formed in the pipe wall of the coagulant aid straight-through pipeline;
the spiral flocculant pipeline is positioned in the flocculation tank and spirally wound outside the coagulant aid straight pipeline, the liquid inlet end of the spiral flocculant pipeline is communicated with one end of a flocculant liquid inlet pipeline penetrating into the flocculation tank, and the liquid outlet end of the spiral flocculant pipeline is communicated with one end of a flocculant liquid outlet pipeline penetrating into the flocculation tank; and a plurality of second liquid outlet holes are uniformly formed in the pipe wall of the spiral pipeline of the flocculating agent.
In the technical scheme, the sewage treatment equipment with high treatment efficiency, long service life and high reliability can be obtained through the application. The flocculant spiral pipeline is spirally wound outside the coagulant aid straight pipeline in the sewage treatment equipment, so that the contact area between flowing sewage and the coagulant aid straight pipeline and the contact area between flowing sewage and the flocculant spiral pipeline can be obviously increased, the coagulant aid and the flocculant discharged from the liquid outlet holes of the coagulant aid straight pipeline and the flocculant spiral pipeline can be quickly and uniformly mixed and melted with the sewage, the sewage subjected to mixing and melting is discharged into the precipitation equipment, the precipitation process of the sewage can be realized, the equipment obtained by the application can be quickly and uniformly mixed and melted, and the sewage treatment efficiency can be obviously improved.
Drawings
FIG. 1 is a graph of the oxidation resistance of a flocculant spiral pipeline material of the present invention as a function of time of use;
FIG. 2 is a schematic diagram of a spiral piping structure of a flocculant according to the present invention;
FIG. 3 is a schematic diagram of a spiral pipe structure of flocculant in the present invention.
In the figure: 1. a flocculation tank, 2, a coagulant aid inlet pipeline, 3, a flocculant inlet pipeline, 4, a cleaning agent inlet pipeline, 5, a coagulant aid outlet pipeline, 6, a flocculant outlet pipeline, 7, a cleaning agent outlet pipeline, 8, a cleaning agent spraying mechanism, 9, a filter disc, 10, a coagulant aid through pipeline, 11, a flocculant spiral pipeline, 12, a spray head, 13, a control system, 14, a coagulant aid inlet valve, 15, a flocculant inlet valve, 16, a cleaning agent inlet valve, 17, a coagulant aid outlet valve, 18, a flocculant outlet valve, 19, a sewage outlet valve, 20, a flocculant inlet temperature detector, 21, a coagulant aid inlet temperature detector, 22, a flocculant outlet concentration detector, 23, a coagulant aid anion concentration detector, 24, a filter screen dirt concentration detector, 25, an outer ring closed pipeline, 26 and a connecting pipeline.
Detailed Description
The invention will be further explained with reference to the drawings.
The spiral pipeline for the flocculating agent comprises the following components in parts by weight:
72-132 parts of bis [2- [ [6- [ (4-chloro-6-methoxy-1, 3, 5-triazin-2-yl) amino ] -1-hydroxy-3-sulfo-2-naphthyl ] azo ] benzoic acid ] chromic acid disodium salt, 62-162 parts of [ 4-hydroxy-3- [ (2-hydroxy-5-nitro-3-sulfophenyl) azo ] -6- [ (sulfomethyl) amino ] -2-naphthalenesulfonato ] sodium chromate, 112-222 parts of 6- [ (5-chloro-2-hydroxy-3-nitrophenyl) azo ] -5-hydroxy-4-phenylamino-1-naphthalenesulfonate monosodium salt, and 112-222 parts of bis [ 6-amino-5- [ (2-hydroxy-3, 22-62 parts of 5-dinitrophenyl) azo ] -1-naphthalenesulfonate (3-1) ] cobalt (III) trisodium, 82-142 parts of N- (2-carboxyl-5-chlorphenyl) -6-methoxy-3-pyridylamine, 42-82 parts of 3-ethyl-5-methyl-4- (2-chlorphenyl) -2- (2, 2-diethoxy-ethoxymethyl) -6-methyl-1, 4-dihydro-pyridine-3, 5-dicarboxylic acid, 62-122 parts of 4-phenyl-6-methyl-5-ethoxycarbonyl-dihydropyridinone with the concentration of 32-62 ppm, and 5-methoxycarbonyl-4- (4-methoxyphenyl) -6-methyl-3, 42-82 parts of 4-dihydropyrimidine-2 (1H) ketone, 122-152 parts of 2, 3-dihydro-2-hydroxy-1, 3, 3-trimethyl-1H-indole-2-carbonyloxyaldehyde (4-methoxyphenyl) methylhydrazone, 72-172 parts of a crosslinking agent, 52-122 parts of 1,3, 3-trimethyl-2-methylene 2, 3-indoline, 32-92 parts of 5-chloro-1, 3, 3-trimethyl-2-methylindoline, 52-142 parts of 5- (4, 6-dimethoxypyrimidin-2-ylcarbamoylsulfamoyl) -1-methylpyrazole-4-carboxylic acid, 1- (4, 6-dimethoxypyrimidin-2-yl) -3- (3-dimethylcarbamoylpyridin-2-yl) Sulfonyl) urea 92-172 parts. The flocculant spiral pipeline of the component has good heat conductivity, high temperature resistance, high pressure resistance and high corrosion resistance, and is long in service life and not easy to damage.
In order to improve various performances of the spiral pipeline of the flocculating agent, the crosslinking agent is any one of 6-ethoxy-3-pyridine methylamine, 2-ethyl-6-methyl-3-hydroxypyridine and 2-hydroxyethyl-3-ethylpyridine.
The invention also provides a preparation method of the spiral pipeline 11 for the flocculant, which comprises the following steps:
the method comprises the following steps: adding 1472-1742 parts of ultrapure water with the conductivity of 3.22 muS/cm-5.22 muS/cm into the reaction kettle, starting a stirrer in the reaction kettle at the rotating speed of 72 rpm-132 rpm, and starting a heating pump to raise the temperature in the reaction kettle to 52-82 ℃; sequentially adding bis [2- [ [6- [ (4-chloro-6-methoxy-1, 3, 5-triazine-2-yl) amino ] -1-hydroxy-3-sulfo-2-naphthyl ] azo ] benzoic acid ] chromic acid disodium salt, [ 4-hydroxy-3- [ (2-hydroxy-5-nitro-3-sulfophenyl) azo ] -6- [ (sulfomethyl) amino ] -2-naphthalenesulfonato ] sodium chromate and 6- [ (5-chloro-2-hydroxy-3-nitrophenyl) azo ] -5-hydroxy-4-phenylamino-1-naphthalenesulfonic acid monosodium salt, stirring until complete dissolution, adjusting the pH value to 4.2-7.2, adjusting the rotation speed of the stirrer to 142-262 rpm at the temperature of 112-152 ℃, and carrying out esterification reaction for 22-32 hours;
step two: crushing di [ 6-amino-5- [ (2-hydroxy-3, 5-dinitrophenyl) azo ] -1-naphthalenesulfonate (3-1) ] trisodium cobalt (III) and N- (2-carboxyl-5-chlorphenyl) -6-methoxy-3-pyridylamine into powder with the particle size of 532-1452 meshes; adding 3-ethyl-5-methyl-4- (2-chlorphenyl) -2- (2, 2-diethoxy-ethoxymethyl) -6-methyl-1, 4-dihydro-pyridine-3, 5-dicarboxylic acid, uniformly mixing, flatly paving in a tray, wherein the flatly paving thickness is 42-62 mm, and irradiating for 72-152 minutes by adopting alpha rays with the dose of 5.2-11.2 kGy and the energy of 6.2 MeV-15.2 MeV and beta rays with the same dose of 62-142 minutes;
step three: dissolving the mixed powder treated in the second step into 4-phenyl-6-methyl-5-ethoxycarbonyl-dihydropyridone, adding the mixture into a reaction kettle, wherein the rotating speed of a stirrer is 82rpm to 192rpm, the temperature is 92 ℃ to 172 ℃, starting a vacuum pump to ensure that the vacuum degree of the reaction kettle reaches-0.04 MPa to-0.09 MPa, and keeping the state to react for 12 to 22 hours; releasing pressure and introducing radon gas to ensure that the pressure in the reaction kettle is 1.32MPa to 1.72MPa, and keeping the temperature and standing for 32 to 42 hours; the rotating speed of the stirrer is increased to 162 rpm-312 rpm, and the pressure of the reaction kettle is reduced to 0 MPa; sequentially adding 5-methoxycarbonyl-4- (4-methoxyphenyl) -6-methyl-3, 4-dihydropyrimidine-2 (1H) ketone, 2, 3-dihydro-2-hydroxy-1, 3, 3-trimethyl-1H-indole-2-carboxaldehyde (4-methoxyphenyl) methylhydrazone to completely dissolve, adding a cross-linking agent, stirring and mixing to ensure that the hydrophilic-lipophilic balance value of the solution in the reaction kettle is 6.2-9.2, and standing for 12-32 hours under heat preservation;
step four: when the rotating speed of a stirrer is 152-232 rpm, sequentially adding 1,3, 3-trimethyl-2-methylene 2, 3-indoline, 5-chloro-1, 3, 3-trimethyl-2-methylindoline, 5- (4, 6-dimethoxypyrimidine-2-yl carbamoylsulfamoyl) -1-methylpyrazole-4-carboxylic acid and 1- (4, 6-dimethoxypyrimidine-2-yl) -3- (3-dimethylcarbamoylpyridine-2-yl sulfonyl) urea, and increasing the pressure of a reaction kettle to 2.12-2.92 MPa, the temperature of the reaction kettle is 152-272 ℃, and carrying out polymerization reaction for 22-32 hours; and after the reaction is finished, reducing the pressure in the reaction kettle to 0MPa, reducing the temperature to 32-52 ℃, discharging, and putting into a molding press for producing a spiral pipeline to obtain the spiral pipeline 11 of the flocculating agent.
The preparation method has simple process, easy realization, difficult environmental pollution and lower requirements on technology and equipment.
Example 1:
the flocculant spiral pipeline 11 is manufactured according to the following steps in parts by weight:
step 1: 1472 parts of ultrapure water with the conductivity of 3.22 mu S/cm is added into the reaction kettle, the stirrer in the reaction kettle is started, the rotating speed is 72rpm, and the heating pump is started to raise the temperature in the reaction kettle to 52 ℃; bis [2- [ [6- [ (4-chloro-6-methoxy-1, 3, 5-triazin-2-yl) amino ] -1-hydroxy-3-sulfo-2-naphthyl ] azo ] benzoic acid ] chromic acid disodium salt 72 parts, [ 4-hydroxy-3- [ (2-hydroxy-5-nitro-3-sulfophenyl) azo ] -6- [ (sulfomethyl) amino ] -2-naphthalenesulfonato ] sodium chromate 62 parts, 6- [ (5-chloro-2-hydroxy-3-nitrophenyl) azo ] -5-hydroxy-4-phenylamino-1-naphthalenesulfonic acid monosodium salt 112 parts are added in sequence, stirred until completely dissolved, adjusting the pH value to 4.2, adjusting the rotation speed of a stirrer to 142rpm at the temperature of 112 ℃, and carrying out esterification reaction for 22 hours;
step 2: 22 parts of trisodium bis [ 6-amino-5- [ (2-hydroxy-3, 5-dinitrophenyl) azo ] -1-naphthalenesulfonate (3-1) ] cobalt (III) and 82 parts of N- (2-carboxyl-5-chlorphenyl) -6-methoxyl-3-pyridylamine are crushed, and the particle size of the powder is 532 meshes; adding 42 parts of 3-ethyl-5-methyl-4- (2-chlorphenyl) -2- (2, 2-diethoxy-ethoxymethyl) -6-methyl-1, 4-dihydro-pyridine-3, 5-dicarboxylic acid, uniformly mixing, flatly paving in a tray, wherein the flatly paving thickness is 42mm, and irradiating for 72 minutes by adopting alpha rays with the dose of 5.2kGy and the energy of 6.2MeV and beta rays with the same dose for 62 minutes;
and 3, step 3: the mixed powder with the concentration of 32ppm treated in the step 2 is dissolved in 62 parts of 4-phenyl-6-methyl-5-ethoxycarbonyl-dihydropyridone, added into a reaction kettle, the rotating speed of a stirrer is 82rpm, the temperature is 92 ℃, a vacuum pump is started to ensure that the vacuum degree of the reaction kettle reaches 1.42MPa, and the reaction is kept for 12 hours in the state; releasing pressure, introducing radon gas to ensure that the pressure in the reaction kettle is 1.32MPa, and keeping the temperature and standing for 32 hours; the rotating speed of the stirrer is increased to 162rpm, and the pressure of the reaction kettle is reduced to 0 MPa; after 42 parts of 5-methoxycarbonyl-4- (4-methoxyphenyl) -6-methyl-3, 4-dihydropyrimidine-2 (1H) ketone and 122 parts of 2, 3-dihydro-2-hydroxy-1, 3, 3-trimethyl-1H-indole-2-carboxaldehyde (4-methoxyphenyl) methylhydrazone are added in sequence and completely dissolved, 72 parts of cross-linking agent are added and stirred and mixed to ensure that the hydrophilic-lipophilic balance value of the solution in the reaction kettle is 6.2, and the solution is kept warm and kept stand for 12 hours;
and 4, step 4: when the rotating speed of a stirrer is 152rpm, sequentially adding 52 parts of 1,3, 3-trimethyl-2-methylene 2, 3-indoline, 32 parts of 5-chloro-1, 3, 3-trimethyl-2-methylene indoline, 52 parts of 5- (4, 6-dimethoxypyrimidin-2-ylcarbamoylsulfamoyl) -1-methylpyrazole-4-carboxylic acid and 92 parts of 1- (4, 6-dimethoxypyrimidin-2-yl) -3- (3-dimethylcarbamoylpyridin-2-ylsulfonyl) urea, and increasing the pressure of a reaction kettle to 2.12MPa, controlling the temperature to be 152 ℃ and carrying out polymerization reaction for 22 hours; after the reaction is finished, reducing the pressure in the reaction kettle to 0MPa, reducing the temperature to 32 ℃, discharging, and putting into a molding press to prepare a spiral pipeline 11 of the flocculating agent;
the cross-linking agent is 6-ethoxy-3-pyridine methylamine.
Example 2:
the flocculant spiral pipeline 11 is manufactured according to the following steps in parts by weight:
step 1: 1532 parts of ultrapure water with the conductivity of 4.52 mu S/cm is added into the reaction kettle, the stirrer in the reaction kettle is started, the rotating speed is 112rpm, and the heating pump is started to raise the temperature in the reaction kettle to 72 ℃; bis [2- [ [6- [ (4-chloro-6-methoxy-1, 3, 5-triazin-2-yl) amino ] -1-hydroxy-3-sulfo-2-naphthyl ] azo ] benzoic acid ] chromic acid disodium salt 112 parts, [ 4-hydroxy-3- [ (2-hydroxy-5-nitro-3-sulfophenyl) azo ] -6- [ (sulfomethyl) amino ] -2-naphthalenesulfonato ] sodium chromate 112 parts, 6- [ (5-chloro-2-hydroxy-3-nitrophenyl) azo ] -5-hydroxy-4-phenylamino-1-naphthalenesulfonic acid monosodium salt 162 parts are added in sequence, stirred until completely dissolved, adjusting the pH value to 6.2, adjusting the rotation speed of a stirrer to 212rpm at the temperature of 132 ℃, and carrying out esterification reaction for 26 hours;
step 2: 42 parts of trisodium bis [ 6-amino-5- [ (2-hydroxy-3, 5-dinitrophenyl) azo ] -1-naphthalenesulfonate (3-1) ] cobalt (III) and 112 parts of N- (2-carboxyl-5-chlorphenyl) -6-methoxyl-3-pyridylamine are crushed, and the particle size of the powder is 1122 meshes; adding 62 parts of 3-ethyl-5-methyl-4- (2-chlorphenyl) -2- (2, 2-diethoxy-ethoxymethyl) -6-methyl-1, 4-dihydro-pyridine-3, 5-dicarboxylic acid, uniformly mixing, flatly paving in a tray, wherein the flatly paving thickness is 52mm, and irradiating for 112 minutes by adopting alpha rays with the dose of 9.2kGy and the energy of 11.2MeV and 122 minutes by adopting beta rays with the same dose;
and 3, step 3: the mixed powder with the concentration of 52ppm processed in the step 2 is dissolved in 92 parts of 4-phenyl-6-methyl-5-ethoxycarbonyl-dihydropyridone, added into a reaction kettle, the rotating speed of a stirrer is 132rpm, the temperature is 142 ℃, a vacuum pump is started to enable the vacuum degree of the reaction kettle to reach 1.62MPa, and the reaction is kept for 17 hours in the state; releasing pressure, introducing radon gas to ensure that the pressure in the reaction kettle is 1.52MPa, and keeping the temperature and standing for 37 hours; the rotating speed of the stirrer is increased to 242rpm, and the pressure of the reaction kettle is reduced to 0 MPa; sequentially adding 62 parts of 5-methoxycarbonyl-4- (4-methoxyphenyl) -6-methyl-3, 4-dihydropyrimidine-2 (1H) ketone and 142 parts of 2, 3-dihydro-2-hydroxy-1, 3, 3-trimethyl-1H-indole-2-carboxaldehyde (4-methoxyphenyl) methylhydrazone into the mixture, completely dissolving the mixture, adding 122 parts of a cross-linking agent, stirring and mixing the mixture to ensure that the hydrophilic-lipophilic balance value of the solution in the reaction kettle is 7.2, and keeping the temperature and standing the mixture for 22 hours;
and 4, step 4: when the rotating speed of a stirrer is 192rpm, sequentially adding 92 parts of 1,3, 3-trimethyl-2-methylene 2, 3-indoline, 62 parts of 5-chloro-1, 3, 3-trimethyl-2-methylene indoline, 92 parts of 5- (4, 6-dimethoxypyrimidin-2-ylcarbamoylsulfamoyl) -1-methylpyrazole-4-carboxylic acid and 132 parts of 1- (4, 6-dimethoxypyrimidin-2-yl) -3- (3-dimethylcarbamoylpyridin-2-ylsulfonyl) urea, and increasing the pressure of a reaction kettle to 2.52MPa, controlling the temperature to be 212 ℃ and carrying out polymerization reaction for 27 hours; after the reaction is finished, reducing the pressure in the reaction kettle to 0MPa, reducing the temperature to 42 ℃, discharging, and putting into a molding press to prepare a spiral pipeline 11 of the flocculating agent;
the cross-linking agent is 2-hydroxyethyl-3-ethylpyridine.
Example 3:
the flocculant spiral pipeline 11 is manufactured according to the following steps in parts by weight:
step 1: 1742 parts of ultrapure water with the conductivity of 5.22 mu S/cm is added into the reaction kettle, the stirrer in the reaction kettle is started, the rotating speed is 132rpm, and the heating pump is started to raise the temperature in the reaction kettle to 82 ℃; adding 132 parts of bis [2- [ [6- [ (4-chloro-6-methoxy-1, 3, 5-triazin-2-yl) amino ] -1-hydroxy-3-sulfo-2-naphthyl ] azo ] benzoic acid ] chromic acid disodium salt, 162 parts of [ 4-hydroxy-3- [ (2-hydroxy-5-nitro-3-sulfophenyl) azo ] -6- [ (sulfomethyl) amino ] -2-naphthalenesulfonato ] sodium chromate and 222 parts of 6- [ (5-chloro-2-hydroxy-3-nitrophenyl) azo ] -5-hydroxy-4-phenylamino-1-naphthalenesulfonic acid monosodium salt in sequence, stirring until complete dissolution, adjusting the pH value to 7.2, adjusting the rotation speed of a stirrer to 262rpm at the temperature of 152 ℃, and carrying out esterification reaction for 32 hours;
step 2: 62 parts of trisodium bis [ 6-amino-5- [ (2-hydroxy-3, 5-dinitrophenyl) azo ] -1-naphthalenesulfonate (3-1) ] cobalt (III) and 142 parts of N- (2-carboxyl-5-chlorphenyl) -6-methoxyl-3-pyridylamine are crushed, and the particle size of the powder is 1452 meshes; adding 82 parts of 3-ethyl-5-methyl-4- (2-chlorphenyl) -2- (2, 2-diethoxy-ethoxymethyl) -6-methyl-1, 4-dihydro-pyridine-3, 5-dicarboxylic acid, uniformly mixing, flatly paving in a tray, wherein the flatly paving thickness is 62mm, and irradiating for 152 minutes by adopting alpha rays with the dose of 11.2kGy and the energy of 15.2MeV and 142 minutes by adopting beta rays with the same dose;
and 3, step 3: the mixed powder with the concentration of 62ppm processed in the step 2 is dissolved in 122 parts of 4-phenyl-6-methyl-5-ethoxycarbonyl-dihydropyridone, added into a reaction kettle, the rotating speed of a stirrer is 192rpm, the temperature is 172 ℃, a vacuum pump is started to enable the vacuum degree of the reaction kettle to reach 1.92MPa, and the reaction is kept for 22 hours in the state; releasing pressure, introducing radon gas to ensure that the pressure in the reaction kettle is 1.72MPa, and keeping the temperature and standing for 42 hours; the rotating speed of the stirrer is increased to 312rpm, and the pressure of the reaction kettle is reduced to 0 MPa; sequentially adding 82 parts of 5-methoxycarbonyl-4- (4-methoxyphenyl) -6-methyl-3, 4-dihydropyrimidine-2 (1H) ketone and 152 parts of 2, 3-dihydro-2-hydroxy-1, 3, 3-trimethyl-1H-indole-2-carboxaldehyde (4-methoxyphenyl) methylhydrazone to completely dissolve, adding 172 parts of cross-linking agent to stir and mix so as to enable the hydrophilic-lipophilic balance value of the solution in the reaction kettle to be 9.2, and preserving heat and standing for 32 hours;
and 4, step 4: when the rotating speed of a stirrer is 232rpm, adding 122 parts of 1,3, 3-trimethyl-2-methylene 2, 3-indoline, 92 parts of 5-chloro-1, 3, 3-trimethyl-2-methylene indoline, 142 parts of 5- (4, 6-dimethoxypyrimidin-2-ylcarbamoylsulfamoyl) -1-methylpyrazole-4-carboxylic acid and 172 parts of 1- (4, 6-dimethoxypyrimidin-2-yl) -3- (3-dimethylcarbamoylpyridin-2-ylsulfonyl) urea in sequence, and increasing the pressure of a reaction kettle to 2.92MPa, controlling the temperature to be 272 ℃ and carrying out polymerization reaction for 32 hours; after the reaction is finished, reducing the pressure in the reaction kettle to 0MPa, reducing the temperature to 52 ℃, discharging, and putting into a molding press to prepare a spiral pipeline 11 of the flocculating agent;
the cross-linking agent is 2-ethyl-6-methyl-3-hydroxypyridine.
Comparative example:
a control example is a commercial flocculant spiral line 11 of a certain brand.
The flocculant spiral pipeline 11 prepared in the examples 1 to 3 and the flocculant spiral pipeline 11 described in the comparative example were compared in terms of use effect. The results of the statistics of the thermal conductivity, the high temperature resistance, the high pressure resistance and the corrosion resistance of the two are shown in table 1.
As can be seen from Table 1, the indexes of the flocculant spiral pipeline 11 prepared by the invention, such as thermal conductivity, high temperature resistance, high pressure resistance, corrosion resistance and the like, are superior to those of products produced by the prior art.
In addition, as shown in FIG. 1, is a statistic of the oxidation resistance of the flocculant spiral pipe 11 material of the present invention as a function of time of use. As shown in the figure, the degree of oxidation resistance of the flocculant spiral pipeline 11 used in the embodiments 1 to 3 is greatly better than that of the existing product along with the change of the use time.
As shown in fig. 2 and fig. 3, the present invention further provides an application of a spiral flocculant pipeline 11 as a component of a sewage treatment apparatus, the sewage treatment apparatus includes a horizontal flocculation tank 1, a coagulant aid inlet pipeline 2 and a flocculant inlet pipeline 3 are respectively arranged on the upper portion of the body of the flocculation tank 1, a cleaning agent outlet pipeline 4 and a flocculant outlet pipeline 6 are respectively arranged on the lower portion of the body of the flocculation tank 1, a cleaning agent inlet pipeline 7 and a coagulant aid outlet pipeline 5 are respectively arranged on the left and right sides of the body of the flocculation tank 1, a cleaning agent spraying mechanism 8, a filter disc 9 and a straight flocculant pipeline 10 are arranged inside the flocculation tank 1, and the flocculation tank 1 is cylindrical; at least one filter screen is arranged in the filter disc 9, and the flocculation tank 1 is divided into a first chamber on the left side and a second chamber on the right side by the filter disc 9; the first chamber is provided with a sewage inlet pipeline communicated with the outside of the flocculation tank 1; a sewage discharge pipeline communicated to the outside of the flocculation tank 1 is arranged at the right end of the second chamber; the cleaning agent spraying mechanism 8 is positioned in the first chamber, a plurality of spray heads 12 are uniformly arranged on the right side of the cleaning agent spraying mechanism 8, and inlet ends of the spray heads 12 are communicated with each other and then communicated with a water outlet end of a cleaning agent liquid inlet pipeline 4 penetrating into the flocculation tank 1; the cleaning agent spraying mechanism 8 is arranged at the water outlet end of the cleaning agent inlet pipeline 4 through a bearing; the coagulant aid through pipeline 10 is positioned in the second chamber; the number of the coagulant aid straight pipelines 10 is multiple, the multiple coagulant aid straight pipelines 10 extend along the length direction of the flocculation tank 1, the liquid inlet ends of the multiple coagulant aid straight pipelines 10 are communicated with each other and then communicated with one end of a coagulant aid liquid inlet pipeline 2 penetrating into the flocculation tank 1, and the liquid outlet ends of the multiple coagulant aid straight pipelines 10 are communicated with each other and then communicated with one end of a coagulant aid liquid outlet pipeline 5 extending into the flocculation tank 1; a plurality of liquid outlet holes I are uniformly formed in the pipe wall of the coagulant aid straight-through pipeline 10; the flocculant spiral pipeline 11 is positioned inside the flocculation tank 1 and spirally wound outside the coagulant aid straight pipeline 10, the liquid inlet end of the flocculant spiral pipeline is communicated with one end of a flocculant liquid inlet pipeline 3 penetrating into the flocculation tank 1, and the liquid outlet end of the flocculant spiral pipeline is communicated with one end of a flocculant liquid outlet pipeline 6 penetrating into the flocculation tank 1; a plurality of second liquid outlet holes are uniformly formed in the pipe wall of the flocculant spiral pipeline 11. The flocculant spiral pipeline 11 is spirally wound outside the coagulant aid straight pipeline 10, so that the contact area between the flowing sewage and the coagulant aid straight pipeline 10 and the contact area between the flowing sewage and the flocculant spiral pipeline 11 can be obviously increased, the coagulant aid and the flocculant discharged from the liquid outlet holes of the coagulant aid straight pipeline 10 and the flocculant spiral pipeline 11 can be quickly and uniformly mixed and melted with the sewage, and the sewage treatment efficiency can be obviously improved. The filter disc 9 can filter out impurities in the sewage; the cleaning agent spraying mechanism 8 can supply cleaning agent through the cleaning agent inlet pipeline 4 when the filter disc 9 needs cleaning, and then the cleaning agent is sprayed on the filter disc 9 by the cleaning agent spraying mechanism 8, so that dirt attached to the filter disc 9 can be effectively cleaned, and the cleaned cleaning agent and the dirt mixed liquid are discharged through the cleaning agent outlet pipeline 7. The sewage coagulation filler has high sewage treatment efficiency, dirt generated in the sewage treatment process in the sewage coagulation filler is easy to clean, and the condition that the sewage treatment efficiency is reduced due to the fact that the dirt in the sewage coagulation filler is cleaned can be effectively reduced. The sewage treatment equipment with high treatment efficiency, long service life and high reliability can be obtained through the application.
In order to automatically control the sewage treatment process, monitor the depth of inlet and outlet liquid in real time and automatically clean dirt on a filter disc, the sewage treatment system also comprises a control system 13, a flocculant inlet temperature detector 20, a coagulant aid inlet temperature detector 21, a flocculant outlet concentration detector 22, a coagulant aid anion concentration detector 23 and a filter screen dirt concentration detector 24; the flocculant inlet temperature detector 20 is arranged at a flocculant inlet inside the flocculation tank 1, the coagulant aid inlet temperature detector 21 is arranged at a coagulant aid inlet inside the flocculation tank 1, the flocculant outlet concentration detector 22 is arranged at a flocculant outlet inside the flocculation tank 1, the coagulant aid anion concentration detector 23 is arranged at a coagulant aid outlet inside the flocculation tank 1, and the screen fouling concentration detector 24 is arranged on a screen in the filter disc 9; a coagulant aid liquid inlet valve 14, a flocculant liquid inlet valve 15, a detergent liquid inlet valve 16, a coagulant aid liquid outlet valve 17, a flocculant liquid outlet valve 18 and a sewage liquid outlet valve 19 are respectively arranged on the coagulant aid liquid inlet pipeline 2, the flocculant liquid inlet pipeline 3, the detergent liquid inlet pipeline 4, the coagulant aid liquid outlet pipeline 5, the flocculant liquid outlet pipeline 6 and the detergent liquid outlet pipeline 7; and a coagulant aid inlet valve 14, a flocculant inlet valve 15, a cleaning agent inlet valve 16, a coagulant aid outlet valve 17, a flocculant outlet valve 18, a sewage outlet valve 19, a flocculant inlet temperature detector 20, a coagulant aid inlet temperature detector 21, a flocculant outlet concentration detector 22, a coagulant aid anion concentration detector 23 and a filter screen dirt concentration detector 24 are all electrically connected with the control system 13.
In order to uniformly spray the cleaning agent on the filter disc 9, the cleaning agent spraying mechanism 8 is in a disc shape and consists of an outer ring closed pipeline 25 and a plurality of radially arranged connecting pipelines 26 communicated between the cleaning agent inlet pipeline 4 and the outer ring closed pipeline 25, and the spray heads 12 are arranged on the connecting pipelines 26 and the outer ring closed pipeline 25.
In order to ensure the filtering effect of the sewage and simultaneously prevent the flow velocity of the sewage from being too slow to reduce the sewage treatment efficiency, 2-3 filter screens are arranged in the filter disc 9, the filter screens are all arranged longitudinally, and a set distance can be arranged between every two adjacent filter screens.
In order to improve the sewage treatment effect, the number of the coagulant aid straight pipelines 10 is 15-20, and the coagulant aid straight pipelines are uniformly distributed along the circumferential direction.
In order to improve the stability and reliability of the coagulation filler, the flocculation tank 1 is made of high-temperature and high-pressure resistant materials.
Preferably, the flocculation tank further comprises a bracket, and the bracket is erected at the bottom of the flocculation tank.
Claims (1)
1. An application device of a spiral flocculant pipeline is characterized in that the spiral flocculant pipeline is used as a component of a sewage treatment device,
the sewage treatment device comprises a flocculation tank (1) which is transversely arranged, wherein a coagulant aid liquid inlet pipeline (2) and a flocculant liquid inlet pipeline (3) are respectively arranged on the upper part of a tank body of the flocculation tank (1), a cleaning agent liquid outlet pipeline (7) and a flocculant liquid outlet pipeline (6) are respectively arranged on the lower part of the tank body of the flocculation tank (1), a cleaning agent liquid inlet pipeline (4) and a coagulant aid liquid outlet pipeline (5) are respectively arranged on the left side and the right side of the tank body of the flocculation tank (1), a cleaning agent spraying mechanism (8), a filtering disc (9) and a coagulant aid straight pipeline (10) are arranged in the flocculation tank (1), and the flocculation tank (1) is cylindrical; the flocculation tank (1) is divided into a first chamber on the left side and a second chamber on the right side by the filter disc (9); the first chamber is provided with a sewage inlet pipeline communicated with the outside of the flocculation tank (1); a sewage discharge pipeline communicated to the outside of the flocculation tank (1) is arranged at the right end of the second chamber; the cleaning agent spraying mechanism (8) is positioned in the first cavity, a plurality of spray heads (12) are uniformly arranged on the right side of the cleaning agent spraying mechanism (8), and inlet ends of the spray heads (12) are communicated with a water outlet end of a cleaning agent liquid inlet pipeline (4) penetrating into the flocculation tank (1); the cleaning agent spraying mechanism (8) is arranged at the water outlet end of the cleaning agent liquid inlet pipeline (4) through a bearing; the coagulant aid through pipeline (10) is positioned in the second chamber; the flocculation tank (1) is provided with a plurality of straight pipelines (10) for coagulant aids, the straight pipelines (10) for coagulant aids extend along the length direction of the flocculation tank (1), the liquid inlet ends of the straight pipelines (10) for coagulant aids are communicated with each other and then communicated with one end of a liquid inlet pipeline (2) for coagulant aids penetrating into the flocculation tank (1), and the liquid outlet ends of the straight pipelines (10) for coagulant aids are communicated with each other and then communicated with one end of a liquid outlet pipeline (5) for coagulant aids extending into the flocculation tank (1); a plurality of liquid outlet holes I are uniformly formed in the pipe wall of the coagulant aid straight-through pipeline (10);
the flocculant spiral pipeline (11) is positioned inside the flocculation tank (1) and spirally wound outside the coagulant aid straight pipeline (10), the liquid inlet end of the flocculant spiral pipeline is communicated with one end of the flocculant liquid inlet pipeline (3) penetrating into the flocculation tank (1), and the liquid outlet end of the flocculant spiral pipeline is communicated with one end of the flocculant liquid outlet pipeline (6) penetrating into the flocculation tank (1); a plurality of liquid outlet holes II are uniformly formed in the pipe wall of the flocculating agent spiral pipeline (11);
the flocculant drying system further comprises a control system (13), a flocculant inlet temperature detector (20), a coagulant aid inlet temperature detector (21), a flocculant outlet concentration detector (22), a coagulant aid anion concentration detector (23) and a filter screen dirt concentration detector (24); the flocculant inlet temperature detector (20) is arranged at a flocculant inlet inside the flocculation tank (1), the coagulant inlet temperature detector (21) is arranged at a coagulant inlet inside the flocculation tank (1), the flocculant outlet concentration detector (22) is arranged at a flocculant outlet inside the flocculation tank (1), the coagulant anion concentration detector (23) is arranged at a coagulant outlet inside the flocculation tank (1), and the screen fouling concentration detector (24) is arranged on a screen in the filter disc (9); the coagulant aid liquid inlet pipeline (2), the flocculant liquid inlet pipeline (3), the cleaning agent liquid inlet pipeline (4), the coagulant aid liquid outlet pipeline (5), the flocculant liquid outlet pipeline (6) and the cleaning agent liquid outlet pipeline (7) are respectively provided with a coagulant aid liquid inlet valve (14), a flocculant liquid inlet valve (15), a cleaning agent liquid inlet valve (16), a coagulant aid liquid outlet valve (17), a flocculant liquid outlet valve (18) and a sewage liquid outlet valve (19); the coagulant aid liquid inlet valve (14), the flocculant liquid inlet valve (15), the cleaning agent liquid inlet valve (16), the coagulant aid liquid outlet valve (17), the flocculant liquid outlet valve (18), the sewage liquid outlet valve (19), the flocculant inlet temperature detector (20), the coagulant aid inlet temperature detector (21), the flocculant outlet concentration detector (22), the coagulant aid anion concentration detector (23) and the filter screen dirt concentration detector (24) are all electrically connected with the control system (13);
the cleaning agent spraying mechanism (8) is disc-shaped and consists of an outer ring closed pipeline (25) and a plurality of radially arranged connecting pipelines (26) communicated between the cleaning agent liquid inlet pipeline (4) and the outer ring closed pipeline (25), and the nozzles (12) are arranged on the connecting pipelines (26) and the outer ring closed pipeline (25);
2-3 filter screens are arranged in the filter disc (9), the filter screens are all arranged longitudinally, and a set distance is reserved between every two adjacent filter screens;
the number of the coagulant aid straight pipelines (10) is 15-20, and the coagulant aid straight pipelines are uniformly distributed along the circumferential direction;
the flocculation tank (1) is made of high-temperature and high-pressure resistant materials;
the flocculation tank further comprises a support, and the support is erected at the bottom of the flocculation tank.
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| CN110041440A (en) * | 2019-05-15 | 2019-07-23 | 石河子大学 | A kind of salt density value flocculant and its preparation method and application |
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|---|---|---|---|---|
| RU2029598C1 (en) * | 1992-06-30 | 1995-02-27 | Акционерное общество "Новатор" | Device for flocculation |
| CN203577414U (en) * | 2013-09-26 | 2014-05-07 | 韩海燕 | Water circulation filter |
| CN205635182U (en) * | 2016-05-19 | 2016-10-12 | 刘飞 | Handle coal mine wastewater's purification tank |
| CN106310826A (en) * | 2016-10-14 | 2017-01-11 | 徐州工程学院 | High-efficiency air purification device in garbage disposal system and operating method thereof |
| CN106365351A (en) * | 2016-10-18 | 2017-02-01 | 徐州工程学院 | Sewage purification device and purification method based on chemical neutralization method and nanofiltration technology |
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2017
- 2017-03-28 CN CN201710193006.9A patent/CN106904710B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2029598C1 (en) * | 1992-06-30 | 1995-02-27 | Акционерное общество "Новатор" | Device for flocculation |
| CN203577414U (en) * | 2013-09-26 | 2014-05-07 | 韩海燕 | Water circulation filter |
| CN205635182U (en) * | 2016-05-19 | 2016-10-12 | 刘飞 | Handle coal mine wastewater's purification tank |
| CN106310826A (en) * | 2016-10-14 | 2017-01-11 | 徐州工程学院 | High-efficiency air purification device in garbage disposal system and operating method thereof |
| CN106365351A (en) * | 2016-10-18 | 2017-02-01 | 徐州工程学院 | Sewage purification device and purification method based on chemical neutralization method and nanofiltration technology |
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